Systems for converting aldose sugars to ketose sugars and separating and/or concentrating these sugars using differences in the sugars' abilities to bind to specific affinity ligands are described.
|
1. A method for converting an aldose in a biomass hydrolysate to its ketose isomer, comprising:
adjusting a ph of a saccharified biomass hydrolysate containing one or more aldose sugars to a value between about 7.5 and about 9, to produce a ph-adjusted hydrolysate;
contacting the ph-adjusted hydrolysate with an isomerization catalyst, wherein at least a portion of the aldose sugar in the ph-adjusted hydrolysate is converted to its ketose isomer, to produce an isomerized hydrolysate;
contacting the ketose isomer in the isomerized hydrolysate with an aryl boronic acid (ABA) at a ph in the range of from 7.5 to 8.5 to form a complex of ketose-conjugate base form of the ABA; wherein the contacting comprises bringing the isomerized hydrolysate into contact with an immiscible organic phase that dissolves the ABA and a lipophilic salt (QX), and allowing the ketose in the isomerized hydrolysate to be extracted into the immiscible organic phase via ester formation with a conjugate base form of the ABA that is coupled via ion pair formation with Q+, thereby reducing the concentration of ketose in the isomerized hydrolysate and forming a ketose-rich organic phase, in turn shifting the aldose/ketose equilibrium in favor of more ketose formation in the ph-adjusted hydrolysate;
preparing a low ph medium having a ph in the range of from about 2 to about 4.5, that contains an acid hx, wherein X is the same anion as X in the lipophilic salt (QX);
bringing the low ph medium into contact with the ketose-rich organic phase; wherein, at the low ph, the ketose and hydroxyl ions are released into the low ph medium and the ABA is converted to its non-ionic conjugate acid; and, wherein, at the same time, the Q+ ion that formed the ion pair combines with an X− ion from the low ph medium to reform the lipophilic salt; and
recovering the ketose from the organic phase into the low ph medium as a concentrated ketose-rich solution.
2. The method of
3. The method of
4. The method of
5. The method of
the shell being configured for containing the organic extraction phase in a shell-side space substantially surrounding the first and second sets of fibers.
6. The method of
7. The method of
8. The method of
passing the hydrolysate through a packed bed reactor containing immobilized xylose isomerase (XI) or solid acid/base catalyst;
allowing the isomerized hydrolysate to flow through the first set of fibers within the micro-porous hollow fiber contactor, the isomerized hydrolysate coming into contact with the immiscible organic phase containing lipophilic ABA and a lipophilic salt (QX) that fills the shell;
extracting the xylulose in the isomerized hydrolysate, wherein the ph of the isomerized hydrolysate is in the range of from 7.5 to 8.5, into the organic phase via ester formation with a conjugate base form of the ABA coupled by ion pair formation with Q+, thereby reducing concentration of xylulose in the hydrolysate, and shifting the xylose/xylulose equilibrium in favor of more xylulose formation;
concurrently with the extracting, allowing the low ph medium to flow through the second set of fibers and contact the organic phase contained on the shell side; whereby:
the xylulose and hydroxyl ions attached to the ABA are released into the low ph medium, the ABA is re-converted to its non-ionic conjugate acid, and
the Q+ ion, which formed the ion pair with ABA, combines with an X− ion from the low ph medium to re-form the lipophilic salt.
9. The method of
10. The method of
11. The method of
12. The method of
13. The method of
14. The method of
15. The method of
16. The method of
17. The method of
18. The method of
a first micro-porous hollow fiber contactor having a lumen side and a shell side, wherein the hydrolyzate flows through the lumen-side in the first micro-porous hollow fiber contactor and the immiscible organic phase flows through the shell-side; and
a second micro-porous hollow fiber contactor that physically separates the ketose-rich organic phase from the low ph medium during ketose recovery.
19. The method of
20. The method of
21. The method of
22. The method of
23. The method of
24. The method of
25. The method of
26. The method of
27. The method of
28. The method of
29. The method of
30. The method of
31. The method of
32. The method of
33. The method of
34. The method of
35. The method of
37. The method of
##STR00011##
wherein A and C are B(OH)2, and B and D are H groups.
39. The method of
##STR00012##
40. The method of
|
|||||||||||||||||||||||||||||||||||||||||||||||||||||||
This application claims the benefit of PCT application No. PCT/US11/033030 filed Apr. 19, 2011, which claims priority to U.S. provisional application, Ser. No. 61/325,710 filed Apr. 19, 2010, the entire disclosure of which is expressly incorporated herein by reference.
This invention was made with government support under GO18163 awarded by the Department of Energy. The government has certain rights in the invention.
Mixed sugar streams, particularly those containing both C5 and C6 sugars, result from hydrolysis of lignocellulosic biomass. Following hydrolysis, these sugars mainly exist in the aldose form. However, ketose isomers of these sugars are typically more amenable to further conversion to useful products and fuels. For example, furans, which form precursors for polymers and hydrocarbon fuels (that could replace gasoline) can be made more easily from the ketose sugars than aldose isomers, and similarly, ethanol can be produced by native yeast through the fermentation the C5 sugar xylose only in its keto-isomer (xylulose) form. As a result, the sugars contained in biomass hydrolysate may need to be converted to their ketose form to facilitate their chemical conversion. The necessary isomerization of aldose to ketose can be achieved by enzymatic (glucose/xylose isomerase (XI)) or chemical (solid acid/base) catalysis. However, the reaction generally favors the aldose form of the sugar and, at equilibrium, only a small portion of the sugar is in the ketose form.
It would be useful to have a system for providing an efficient aldose-ketose transformation and/or separation of C5 and C6 sugars from biomass materials.
Systems for converting aldose sugars to ketose sugars and separating and/or concentrating these sugars using differences in the sugars' abilities to bind to specific affinity ligands are described.
In a broad aspect, there are provided systems for converting aldose sugars to ketose sugars and separating and/or concentrating these sugars. In general, the system includes using differences in the sugars' abilities to bind to specific affinity ligands.
In a broad aspect, there is provided herein system for converting an aldose sugar to its ketose sugar, comprising:
a) contacting a C5 and/or C6 aldose sugar present in a saccharified hydrolysate with a catalyst to form a ketose isomer of the C5 and/or C6 sugar;
b) contacting isomerized ketose C5 and/or C6 sugar with a complexing agent (CA) to form to a ketose-CA conjugate; the CA have a binding affinity more specific to the ketose sugar compared to the aldose sugar;
c), optionally, repeating steps a) and b) to provide a concentrated hydrolysate having more ketose-CA conjugate than aldose sugar; and
d) isolating ketose sugar from the ketose-CA conjugate in the concentrated hydrolysate; and
e) recovering the ketose sugar.
In certain embodiments, the system includes removing ketose from hydrolysate to overcome an unfavorable equilibrium ratio of aldose:ketose (e.g., xylose:xylulose). Also, in certain embodiments, the aldose sugars are present in lignocellulosic biomass hydrolysates.
In certain embodiments, the ketose sugars are isolated by: lowering pH of the concentrated hydrolysate to effect the release of the ketose from the ketose-CA conjugate; and converting the CA to a lipophilic conjugate acid form.
In certain embodiments, wherein the saccharified hydrolysate has a pH between about 7.5 to about 9 when the catalyst comprises xylose isomerase (XI).
In certain embodiments, the saccharified hydrolysate has a pH between about 7.5 to about 11 when the catalyst comprises a zeolite catalyst.
In certain embodiments, the CA is present in an immiscible organic phase that is physically separated by a permeable device from the isomerized hydrolysate, and the permeable device allows transport of the CA into (and out of) the isomerized hydrolysate, while substantially preventing transport of the immiscible organic phase.
In certain embodiments, the immiscible organic material comprises one or more of as ethyl acetate, dichloromethane, o-nitrophenyl octyl ether (NPOE), and or diethyl ether.
In certain embodiments, the system can include: passing the hydrolysate through a packed bed reactor containing an immobilized xylose isomerase (XI) or zeolite catalyst, where xylose present as the aldose sugar in the hydrolysate is converted to its ketose isomer, xylulose.
In certain embodiments, the CA is present in an organic phase, the xylulose extracting the complexing agent (CA) from the organic phase via ester formation with a conjugate base form of the CA.
In certain embodiments, the system can include extracting the CA from the organic phase and allowing the ester formation until nearly all of the xylose is isomerized.
In certain embodiments, the system includes:
acidifying the isomerized hydrolysate containing the ketose-CA conjugate to a pH that favors the conjugate acid form of the CA, such that the conjugate acid form of the CA dissociates from the ketose, and the dissociated ketose increases the hydrophobicity of the CA in the isomerized hydrolysate, and
driving the conjugate acid form of the CA back into the organic phase, thereby forming a CA-depleted/ketose-rich hydrolysate.
In certain embodiments, the system includes: acidifying the CA-depleted/ketose-rich hydrolysate to a pH at which the ketose sugar can be fermented to ethanol by S. cerevisiae, or other native microorganisms.
In certain embodiments, the system can include driving the hydrophobic CA back into the organic phase to form a CA-enriched organic phase, and contacting the CA-enriched organic phase with a fresh batch of saccharified hydrolysate.
In certain embodiments, the system can include: immobilizing the complexing agent (CA) to a support material.
In certain embodiments, one or more of the CA, the pH and temperature of the hydrolysate, are altered to select for one or more specific sugars.
In certain embodiments, the system can include: selecting the CA such that, at selected pH and temperature conditions, the CA mainly binds to xylulose, and not binds any appreciable amounts of glucose, xylose or fructose.
In certain embodiments, the system can include: circulating the hydrolysate through at least a first column comprised of a packed bed of immobilized xylose isomerase (XI) or zeolite catalyst, and through a vessel having a CA-enriched material therein. It is to be understood, that in certain embodiments, this can include the immobilized C; and, in certain embodiments, a hollow fiber module with a CA-organic phase.
In certain embodiments, the system can include: circulating the hydrolysate through at least a first column comprised of a packed bed of immobilized xylose isomerase (XI) or zeolite catalyst particles, and through a second column comprised of a packed bed of a complexing agent (CA) immobilized on a support material.
In certain embodiments, as the hydrolysate passes through the XI column, xylose and a portion of glucose present in the hydrolysate are converted to corresponding keto-isomers (xylulose and fructose, respectively).
In certain embodiments, as the hydrolysate mixture is routed through the immobilized CA column, mainly the ketose will complex with bound CA sites, thereby lowering free ketose concentration in the hydrolysate.
In certain embodiments, the system can include: circulating the hydrolysate through two-columns connected in series.
In certain embodiments, the system can include: isolating the immobilized CA column and flushing the immobilized CA column with a carrier solution of low pH sufficient for bound ketose to be released from the CA and to accumulate in the low pH carrier solution. In certain embodiments, the pH is about 4.0 to about 4.5. Further, in certain embodiments, the pH can corresponds to a pH of a fermentation medium suitable for converting xylulose to ethanol by native S. cerevisiae, or other native microorganisms.
In certain embodiments, the system can include: regenerating the immobilized CA column and reusing with a fresh batch of hydrolysate.
In certain embodiments, the system can include: controlling a volume of the low pH carrier sufficient to recover the ketose as a “concentrated” solution.
In certain embodiments, the system can include: separating the xylose from other C6 sugars as its keto-isomer and allowing for the recovery of xylulose as a concentrated solution.
In certain embodiments, the system can include: a lipophilic salt with the complexing agent (CA) in the organic phase, and extracting the ketose out of the organic phase.
In certain embodiments, the system can include: passing the isomerized hydrolysate and the CA containing organic phase through a hollow fiber contained liquid membrane contactor (HFCLMC).
In certain embodiments, the complexing agent (CA) comprises a complexing agent soluble in organic solvents and/or capable of being covalently-bound to a solid substrate.
In certain embodiments, the complexing agent (CA) comprises one or more of aryl boronic acids (ABAs), including, but not limited to PBA, 3aPBA, 4cPBA and 4-biphenylboronic acid,
##STR00001##
In certain embodiments, the complexing agent (CA) comprises one or more aryl boronic acids (ABA), Ar—B(OH)2, where Ar represents unsubstituted or substituted “aryl” group.
In certain embodiments, the aryl boronic acids (ABA), comprise one or more of the following aryl groups: 4-MeC6H4—, where Me is methyl; 2-iPrC6H4—, where iPr is isopropyl; 2-naphthyl, 3-BnOC6H4—, where Bn is benzyl; 4-MeO2CC6H4—, where Me is methyl; and 4-pyridinyl.
In certain embodiments, one or more functional groups such as NH2 or COOH are incorporated into the aryl group to enable covalent bonding of the aryl boronic acids to a functionalized support. Further, in certain embodiments, functionalization of the support includes one or more of: oxirane, amine, carboxyl or other complementary groups that covalently attaches to the functional group on the aryl boronic acid.
In certain embodiments, the ABA comprises a hydrophobic substituted aryl boronic acid. Non-limiting examples include wherein the ABA comprises:
##STR00002##
In certain embodiments, the hydrophobic substituted aryl boronic acid is used in a liquid-liquid extraction followed by stripping or HFCLMC implementation.
In certain embodiments, the ABA comprises a compound that exhibits a higher selectivity toward ketose binding compared to monoboronic acids.
In certain embodiments, the ABA comprises a multi-dentate boronic acid carrier.
In certain embodiments, the ABA compound comprises one or more of:
##STR00003##
wherein A and C are B(OH)2 and B and D are H groups.
In certain embodiments, the complexing agent (CA) comprises one or more unsubstituted or organosubstituted germanate compounds.
In certain embodiments, the CA is contained in a holding vessel that includes a contacting device that physically separates the hydrolysate from the organic phase while allowing movement of the CA into and out of the hydrolysate. Further, in certain embodiments, the contacting device can comprise a CA permeable membrane. Also, in certain embodiments, the contacting device can comprise a microporous hollow fiber contactor.
In certain embodiments, the system can be as shown in
In a particular aspect, there is provided herein a system for converting an aldose in a biomass hydrolysate to its ketose isomer and for making the ketose available for fermentation reactions at an appropriate pH, comprising:
1a) adjusting a pH of a saccharified biomass hydrolysate containing one or more aldose sugars to a value between about 7.5 and about 11;
1b) contacting the pH-adjusted-hydrolysate of step 1a) with a catalyst where at least a portion of the aldose sugar in the pH-adjusted-hydrolysate is converted to its ketose isomer;
2a) contacting the ketose isomer in the isomerized-hydrolysate of step 1b) with a complexing agent (CA) to form a ketose-conjugate base form of the CA;
2b) optionally, repeating steps 1)-2a) as needed, until a desired concentration of the aldose in the isomerized-hydrolysate is converted into an esterified ketose-CA conjugate;
3) ceasing the isomerization cycle of steps 1a)-2b);
4) separating the esterified ketose-CA conjugate from the isomerized-hydrolysate by acidifying the isomerized-hydrolysate to a pH (optionally, between about pH 2 to about 4.5) that favors formation of a conjugate acid form of the CA, causing the CA to dissociate from the ketose; and,
5) contacting the ketose-rich hydrolysate of step 4) with CA-depleted organic material, causing the dissociated CA to be separated from the ketose-rich hydrolysate; and optionally,
6) recovering the dissociated CA material and returning to the organic material of step 2a).
In certain embodiments, the ketose present in the isomerized hydrolysate extracts the CA from the organic material via ester formation with a conjugate base form of the CA, thereby shifting the aldose/ketose equilibrium in favor of more ketose formation in the isomerized hydrolysate.
In certain embodiments, the system can be as shown in
In another aspect, there is provided herein a system for converting an aldose in a biomass hydrolysate to its ketose isomer and for making the ketose available for fermentation reactions at an appropriate pH, comprising:
incorporating an immobilized xylose isomerase XI (or solid acid/base catalyst) column in an extraction step,
converting xylose to xylulose at high yield and high selectivity over glucose to fructose, and
separating xylulose from glucose by binding xylulose to an aryl boronic acid.
In yet another aspect, there is provided herein a system for converting an aldose in a biomass hydrolysate to its ketose isomer and for making the ketose available for fermentation reactions at an appropriate pH, comprising:
1a) adjusting a pH of a saccharified biomass hydrolysate containing one or more aldose sugars to a value between about 7.5 and about 11;
1b) contacting the pH-adjusted-hydrolysate of step 1a) with a catalyst where at least a portion of the aldose sugar in the pH-adjusted-hydrolysate is converted to its ketose isomer;
2) contacting the ketose isomer in the isomerized-hydrolysate of step 1b) with a complexing agent (CA) to form a ketose-conjugate base form of the CA; wherein the contacting comprises
3) bringing the isomerized hydrolysate from the packed bed reactor into contact with an immiscible organic phase that dissolves the CA and a lipophilic salt (such as a quaternary ammonium salt QX); and
allowing the ketose in the isomerized hydrolysate to be extracted into the organic phase via ester formation with a conjugate base form of the CA that is coupled to an ion pair formation with Q+, thus reducing the concentration of uncoupled ketose in the hydrolysate, and shifting the aldose/ketose equilibrium in favor of more ketose formation;
4) preparing an aqueous medium having a pH is in the range of about 2 to about 4.5 that contains an acid HX (where X is the same anion as that of the lipophilic salt) for stripping of the xylulose from the organic phase generated in step 3;
5) bringing the low pH aqueous medium into contact with the ketose-rich organic phase from step 3); wherein, at the low pH, the both ketose and hydroxyl ion are released into the aqueous phase and the CA is converted to its non-ionic conjugate acid; and, wherein, at the same time, the Q+ ion that formed the ion pair combines with an X− ion from the aqueous medium to re-form the lipophilic salt; and
6) recovering the ketose from the ketose-rich organic phase.
In certain embodiments, the system can include: controlling the volume of the aqueous medium such that the concentration of ketose is higher than the initial concentration of aldose in the hydrolysate.
In certain embodiments, the system can include: reusing the regenerated organic phase containing the CA and the lipophilic salt for a next batch of hydrolysate.
In another aspect, there is provided herein a system substantially as shown in
In certain embodiments, the system can include: combining the isomerization step with the selective simultaneous extraction step using a hollow fiber contained liquid membrane contactor (HFCLMC) system.
In certain embodiments, the HFCLMC system comprises a shell having a first set of porous hollow fibers adapted for carrying isomerized hydrolysate; and a second set of porous hollow fibers adapted for carrying an aqueous medium. The shell can be configured for containing the organic extraction phase in a shell-side space substantially surrounding the first and second sets of fibers. In certain embodiments, the separate sets of microporous hollow fibers are commingled within the shell.
In certain embodiments, the xylulose is transported from a high pH medium to a low pH medium across the contained organic liquid membrane, wherein the transport of xylulose is facilitated through the organic film by the dissolved CA and QX combination.
In certain embodiments, the wherein saccharified biomass hydrolysate containing glucose and xylose is passed through a packed bed reactor containing immobilized xylose isomerase (XI) or solid acid/base catalyst;
the isomerized hydrolysate flowing through the first set of fibers within the HFCLMC, the isomerized hydrolysate coming into contact with the immiscible organic phase containing lipophilic CA and a lipophilic salt (QX), that fills the shell;
the xylulose in the isomerized hydrolysate being extracted into the organic phase via ester formation with a conjugate base form of the CA coupled to ion pair formation with Q+, thus reducing concentration xylulose in the hydrolysate, and shifting the xylose/xylulose equilibrium in favor of more xylulose formation;
the low pH aqueous medium having an acid HX (where X is the same anion as that of the lipophilic salt (QX) concurrently flows through the second set of fibers and also contacts the organic phase contained on the shell side; the xylulose and hydroxyl ion are released into the aqueous phase and the CA is re-converted to its non-ionic conjugate acid; and the Q+ ion, which formed the ion pair, combines with an X− ion in the aqueous medium to re-form the lipophilic salt.
In certain embodiments, the system can include: immobilizing the complexing agent CA to a solid support material, such that the immobilized CA acts as a solid-phase extraction medium.
In certain embodiments, the system can include: selecting a CA having a property to enhance selectivity for a specific sugar.
In certain embodiments, the system can include: removing the bound sugar from the hydrolysate medium by contacting the support material with a lower pH solution to achieve separation from the hydrolysate.
In another aspect, there is provided herein a system substantially as shown in
In an other aspect, there is provided herein a system of separating xylose (in the form of its keto-isomer, xylulose) from a biomass hydrolysate containing a mixture of glucose and xylose; comprising:
circulating the biomass hydrolysate through a first column comprised of a packed bed of immobilized xylose isomerase (XI) or solid acid/base catalyst particles; and a second column comprised of a packed bed of a complexing agent (CA) immobilized on a support material; the CA and its binding chemistry to the support material being chosen that the CA substantially binds to xylulose, and not in any appreciable amounts to glucose, xylose or fructose;
passing the hydrolysate through the first (XI) column 51 such that, xylose and a portion of glucose are converted to their corresponding keto-isomers (xylulose and fructose, respectively);
passing the isomerized hydrolysate through the immobilized CA second column 52,
wherein the xylulose complexes with bound CA sites, thereby lowering the xylulose concentration in the hydrolysate, and the reduction in concentration of non-bound xylulose in the isomerized hydrolysate drives the isomerization reaction in the direction of more xylulose formation; and
optionally, isolating the second immobilized CA column and contacting the second (CA) column with a low pH carrier medium, so the bound xylulose is released from the CA sites and accumulates in the low pH carrier medium.
In certain embodiments, the system can further including controlling the volume of the low pH aqueous solution such that xylulose concentration in the recovered stream is higher than the xylose concentration in the original hydrolysate.
Further, in certain embodiments, the system can include an immobilized CA column to recover both glucose and xylose from the hydrolysate by binding glucose and xylose to appropriately chosen CA, and recovering glucose and xylose from the hydrolysate, while leaving behind other inhibitory compounds in the biomass hydrolysate.
In another aspect, there is provided herein use of concentrated ketose streams formed using a system as described herein in a fermentation process to produce a fuel such as ethanol.
In another aspect, there is provided herein use of concentrated ketose streams formed using a system as described herein in a fermentation process to produce chemicals such as succinic and fumaric acids.
In another aspect, there is provided herein a fuel formed by a system as described herein.
Other systems, methods, features, and advantages of the present invention will be or will become apparent to one with skill in the art upon examination of the following drawings and detailed description. It is intended that all such additional systems, methods, features, and advantages be included within this description, be within the scope of the present invention, and be protected by the accompanying claims.
Described herein are methods for the transformation of aldose-ketose for the separation and/or chemical conversion of C6 and C5 sugars from biomass materials. In certain embodiments, the biomass materials are lignocellulosic biomass hydrolysate.
Provided herein is a method for improving yield of aldose-ketose transformations of biomass sugars; isomerization and separation of sugars; conversion of biomass sugars to ethanol with native yeasts.
Also provided herein is a lignocellulosic biomass refining process. Biofuels, biobased products, purified consumable sugars, purified high-value sugars can thus be produced by one or more of the systems, methods and apparatuses described herein.
The system described herein for concentrating sugars from biomass is less energy-intensive than conventional evaporation; moreover, concentrated sugars are obtained free of fermentation inhibitors present in the hydrolysate.
Following separation, the separated sugar/s is in a ketose form that is readily amenable to further biological and or chemical conversion.
In certain embodiments, the process can include recovering the separated sugars as concentrated solutions.
The resulting concentrated individual sugar streams are useful as initially recovered. The resulting concentrated individual sugar streams can be used for human and/or animal consumption.
Also, the resulting concentrated individual sugar streams are useful as feedstocks for production of fuels and chemicals.
In the system described herein the concentration of free xylulose in the hydrolysate is reduced, and there is a shift in the xylose/xylulose equilibrium in favor of more xylulose formation.
One class of sugar-binding, or complexing, agents (CA) include aryl boronic acids, Ar—B(OH)2, where Ar represents an “aryl” group. For example,
##STR00004##
4-biphenylboronic acid or Ar=4-PhC6H4—
Other Ar groups can include, but are not limited to: 4-MeC6H4—, where Me is methyl; 2-iPrC6H4—, where iPr is isopropyl; 2-naphthyl, 3-BnOC6H4—, where Bn is benzyl; 4-MeO2CC6H4—; 4-pyridinyl.
Functional groups such as NH2 or COOH can be incorporated into the aryl group to enable covalent bonding of the aryl boronic acids to functionalized supports. Functionalization of the support can include oxirane, amine, aldehyde, carboxyl or other complementary groups that can covalently attach to the functional group on the aryl boronic acid.
Another more hydrophobic substituted aryl boronic acid that is particularly useful in liquid-liquid extraction followed by stripping or HFCLMC implementation is the compound shown below:
##STR00005##
Compounds that may exhibit higher selectivity toward ketose binding compared to monoboronic acids are multi-dentate boronic acid carriers. Several examples of these compounds are shown in the structures below.
##STR00006##
For the last structure on the above, A and C are B(OH)2 and B and D are H groups.
All the mono and multidentate structures described above are based on the affinity of boronate compounds towards sugars. As shown in one of our examples, germanates are also able to bind selectively to ketose sugars. Thus, chemistries that replace boronate with germanate will also form suitable complexing agents for implementation of the methods described herein.
In the methods described herein, the selective affinity of ketoses to complexing agents is now used to produce high ketose yields, while simultaneously allowing recovery and reuse of the complexing agent and the isomerization catalyst. In addition, in certain embodiments, the method is useful for sugar separation and/or concentration.
While enzyme-catalyzed biochemical means of affecting aldose-ketose transformation has been described in the examples herein, it is to be understood that the isomerization can also be achieved through chemical means at elevated pH and or elevated temperatures where the aldose-ketose selectivity of CAs can be much higher, enabling higher ketose yields as well as better separation of ketose from aldose, using one or more of the methods described herein.
Thus, in a non-limiting manner, in the examples herein, the isomerization and separations were done at 50° C. and at 34° C., and it was observed that XI shows several orders of magnitude higher catalytic performance towards aldose-ketose conversion of C5 sugars compared to C6 sugars in this temperature range. This preference for C5 sugars can also be seen at higher temperatures (for example, at temperatures up to about 60° C.).
Method I:
Shifting the Aldose/Ketose Isomerization Reaction to Achieve High Ketose Yields
Phase Switching:
Borax, aryl boronic acids (ABA) and their derivatives, multidentate boronic acids and other oxyanion compounds can act as complexing agents (CA) by preferentially binding with the ketose forms of both C5 and C6 sugars.
One class of complexing agents that can exhibit pH-dependent partitioning between aqueous and organic phases is aryl boronic acids (ABAs). At high pH (>7.5), ABAs exist predominantly in their conjugated base form (see equations (1) and (2) in
Implementation of Method I—Phase-Switching of CA
In general, the isomerization of aldose to ketose can be been achieved using the enzyme catalyst xylose isomerase (XI) in the pH of 7.5-9.0. Also, solid-state acid/base catalysts can be used for aldose to ketose transformation. Examples of the basic-type catalysts include carbonate and hydroxide forms of hydrotalcite and cation-exchanged hydrotalcites and zeolites. Tin-containing zeolites are solid acid catalysts that can be used for isomerization of glucose to fructose in water. Certain advantages of zeolite catalysts over enzyme catalysts include: (1) relativity inexpensive inorganic compounds; (2) wider range of temperature and pH operating conditions as well as longer lifetimes; (3) faster reaction rates; and (4) increased resistance to impurities.
However, regardless of the nature of the catalyst, the aldose/ketose isomerization does not have a favorable equilibrium.
Although XI is capable of converting xylose to xylulose, under conditions where XI has significant activity, the equilibrium ratio of xylose:xylulose is typically high (on the order of 5:1). Hence, xylose isomerization does not have a favorable forward equilibrium (see Eq. 3 below).
##STR00007##
One way to increase xylose conversion is to drive the isomerization forward by removal of the product xylulose. When the xylulose preferentially binds to the conjugate base of the ABA (see Eq. 1 in
The inventors herein have now developed a method to achieve high conversion of the xylose in biomass hydrolysate to its ketose isomer xylulose and make the sugar available to the fermentation reactions at an appropriate pH.
FIG. 2—Step 1: Saccharified biomass hydrolysate 20 (at pH 4.5 and 50° C.), containing glucose and xylose, is filtered to remove lignin and other particulates and the pH is raised to a value between 7.5 and 9 through addition of a suitable base. The hydrolysate is passed through a packed bed reactor 22 containing immobilized xylose isomerase (XI) where xylose is converted to xylulose. For solid acid/base catalysts, the operational temperature (25-100° C.) and pH range (up to 11) is much broader than that of the XI enzyme.
FIG. 2—Step 2: The partially isomerized hydrolysate from the packed bed reactor 22 is brought into contact with an immiscible organic phase (such as ethyl acetate, dichloromethane, o-nitrophenyl octyl ether (NPOE) or diethyl ether) containing the complexing agent (CA), viz ABA, in a holding vessel 24 which includes a contacting device 25 that physically separates the hydrolysate from the organic phase while allowing transport of the CA between the two phases. In certain embodiments, the contacting device 25 can be a microporous hollow fiber contactor).
The xylulose formed in the isomerization reaction will extract the CA from the organic phase into the hydrolysate via ester formation with the conjugate base form of the CA. This, in effect, reduces the concentration of “free” xylulose in the hydrolysate, shifting the xylose/xylulose equilibrium in favor of more xylulose formation (see Eq. 3). As the hydrolysate repeatedly passes through the immobilized XI (or solid acid/base catalyst) column 22, the extraction of CA from the organic phase and ester formation in the aqueous phase continues until nearly all of the xylose is isomerized. With the solid acid/base catalyst, isomerization temperature and pH conditions are more flexible and can be set to allow for higher and more selective sugar binding to the CA.
FIG. 2—Step 3: At this stage, the isomerized hydrolysate (predominantly xylulose and glucose) is transferred to another vessel 26.
FIG. 2—Step 4: The hydrolysate is acidified to bring the pH down to 2 to 4.5; this pH favors the conjugate acid form of the CA, in which state it no longer associates with the xylulose and the ester breaks down (see
FIG. 2—Step 5: The acidified hydrolysate is pumped through another module 28 where it is brought into contact with the CA-depleted organic phase from Step 2, when the CA has been removed from the holding vessel 24. In the conjugate acid form, the CA is preferentially back-extracted into the organic phase, enriching the organic phase in CA.
FIG. 2—Step 6: The CA-laden organic phase from Step 5 can be sent back to the contacting device 25 in Step 2. Thus, the CA is extracted from the organic phase to the aqueous phase when the pH is high and is back-extracted into the organic phase from the aqueous phase when the pH is low. This “phase-switching” of CA is enhanced significantly in the presence of the ketose sugars at high pH. Phase-switching allows for the continuous recycling and reuse of both the organic phase and the CA.
FIG. 2—Step 7: Following the removal of the CA from the isomerized hydrolysate into the organic phase, the isomerized hydrolysate adjusted to a pH of 4.5 can be cooled to 34° C. and fermented to ethanol using native yeast. This cooling step can be integrated with other heating needs in the process to achieve thermal efficiencies.
Implementation of Method I—Interfacial Complexation
As the lipophilic character of the ABA increases, its ability to undergo phase-switching will diminish. However, it may still form a tetragonal boronic acid ester at the organic/aqueous interface and accumulate at the interface like a surfactant when the aqueous phase it contacts is at high pH. Nevertheless, binding of ABA to xylulose at the liquid-liquid interface will still effectively shift the xylose/xylulose equilibrium toward more xylulose formation. In such situations, there might be no phase-switching mechanism in operation. However, as shown in
For example, following completion of isomerization, the XI column is disconnected from the closed loop on the left side of
Method II—Simultaneous Aldose/Ketose Isomerization and Separation/Concentration of Pentose and Hexose Sugars
Liquid-Liquid Extraction of Sugars:
ABA can be confined to the organic phase by adding lipophilic quaternary ammonium salts such as Aliquat® 336 (Q+X−) to the organic phase. As ABA in the organic phase approaches the high pH aqueous interface, it converts from conjugate acid to conjugate base form; in the conjugate base form it is able to bind readily with sugar at the aqueous/organic interface.
The lipophilic ammonium cation (Q+) will form an ion pair with this tetragonal ABA-sugar ester anion, thereby extracting the tetragonal ester into the organic phase while the anion X− of Aliquat® 336 is liberated into the aqueous phase. Contacting the sugar-loaded organic phase with a low pH aqueous phase containing the acid HX enables stripping of the sugar back to the aqueous media with the uptake of X− into the organic phase as the co-anion of Q+. In this mode of action, the ABA is facilitating the extraction of sugar from the aqueous phase into the organic phase while the ABA itself is confined to the organic phase. This is in contrast to the Method I Phase-Switching where the sugar is confined to the aqueous phase and the ABA is extracted from the organic phase into the aqueous phase and vice versa.
Unlike Method I, extraction of the sugar to a second phase with subsequent stripping can facilitate separation and concentration of sugar. In the past, immiscible liquid extraction was implemented in a two-step process, where in Step 1 xylose and/or glucose are extracted from a high-pH biomass hydrolysate into an organic phase, and in Step 2 the sugars are released into a low pH aqueous stripping solution. Until now, however; there has been no solution for the separation of the C6 from C5 sugars or for the separation of ketose from aldose sugars.
Implementation of Method II—Isomerization Coupled to Selective Liquid-Extraction and Stripping
FIG. 3—Step 1: Saccharified biomass hydrolysate 30 (at pH 4.5 and 50° C.), containing glucose and xylose, is filtered to remove lignin and other particulates and the pH is raised to a value between 7.5 and 9 through addition of a suitable base. The hydrolysate is passed through a packed bed reactor 32 containing immobilized xylose isomerase (XI) (or solid acid/base catalyst) where xylose is converted to xylulose.
FIG. 3—Step 2: The partially isomerized hydrolysate from the backed be reactor 32 is brought into contact with an immiscible organic phase that dissolves a lipophilic ABA and a quaternary ammonium salt (QX, such as Aliquat® 336) in a holding vessel 34 that includes a contacting device 35 that physically separates the hydrolysate from the organic phase while allowing transport of the sugar between the two phases. In certain embodiments, the contacting device 35 can be a microporous hollow fiber contactor. As discussed in the liquid-liquid extraction of sugars, the xylulose formed in the isomerization reaction is extracted into the organic phase via ester formation with the conjugate base form of the CA, which then forms an ion pair with Q+. This, in effect, reduces the concentration of “free” xylulose in the hydrolysate, shifting the xylose/xylulose equilibrium in favor of more xylulose formation (see Eq. 3).
As the hydrolysate repeatedly passes through the immobilized XI (or solid acid/base catalyst) column 32, the extraction of xylulose to the organic phase continues until nearly all of the xylose is isomerized. The XI enzyme catalyzes xylose/xylulose transformation at a rate one-to-two orders of magnitude faster than the glucose/fructose transformation. Hence, during the time required for xylose isomerization, glucose is minimally isomerized (e.g., see data in
The majority of glucose is not extracted into the organic phase due to the vast affinity difference between glucose and xylulose toward ABA (e.g., see data in
FIG. 3—Step 3: Following the isomerization and extraction in Step 2, the extraction loop is shut down. The hydrolysate remaining in the vessel 30 contains predominantly glucose; the organic phase contains the bulk of the initial xylose in the form of xylulose complexed to ABA.
FIG. 3—Step 4: A low pH aqueous medium 36 in the pH range of 2-4.5 is prepared with the acid HX (where X is the same anion as that of the lipophilic ammonium salt) for stripping of the xylulose from the organic phase generated in Step 3.
FIG. 3—Step 5: The low pH aqueous medium 36 is pumped through another module 38 where it is brought into contact with the xylulose-rich organic phase from Step 3. At the low pH, bound xylulose and a hydroxyl ion are released from the complex into the aqueous phase and the ABA gets converted to its non-ionic conjugate acid (see Eq. 2). At the same time, the Q+ ion that formed the ion pair with the complex will combine with an X− ion from the aqueous medium to form the lipophilic ammonium salt.
FIG. 3—Step 6: At the end of the stripping process, the concentrated xylulose-rich medium is used for subsequent conversion to product. By controlling the volume of stripping medium used, the concentration of xylulose can be higher than the initial concentration of xylose in the hydrolysate. The regenerated organic phase containing the ABA and the lipophilic ammonium salt can be reused and recycled for the next batch of hydrolysate.
Implementation of Method II—Isomerization Coupled to Selective Simultaneous Extraction and Stripping in a Hollow Fiber Contained Liquid Membrane Contactor (HFCLMC)
One embodiment of a HFCLMC for the separation of glucose from xylulose and concentration of xylulose is shown in
The hydrolysate is passed through a packed bed reactor 32 containing immobilized XI (or solid acid/base catalyst) (unit 2) where xylose is converted to xylulose. The partially-isomerized hydrolysate flows through the set of dark gray fibers 42 within the HFCLMC (unit 3) where it comes into contact with an immiscible organic phase containing a lipophilic ABA and a quaternary ammonium salt (QX, such as Aliquat® 336) that fills the shell side of the fibers (unit 5). The xylulose formed in the isomerization reaction will be extracted into the organic phase via ester formation with the conjugate base form of the CA coupled to ion pair formation with Q+. This in effect reduces the concentration of “free” xylulose in the hydrolysate, shifting the xylose/xylulose equilibrium in favor of more xylulose formation (Eq. 3).
A low pH aqueous medium 36 (unit 4) in the pH range of 2-4.5 is prepared with the acid HX (where X is the same anion as that of the lipophilic ammonium salt) for stripping of the xylulose from the organic phase in the HFCLMC. This low pH aqueous solution concurrently flows through the second set of fibers 41 (light gray) and also contacts the organic phase contained on the shell side. At the low pH interface, bound xylulose and a hydroxyl ion are released from the complex into the aqueous phase and the ABA gets converted to its non-ionic conjugate acid (see Eq. 2).
At the same time, the Q+ ion that formed the ion pair with the complex will combine with an X− ion from the stripping medium to form the lipophilic ammonium salt. Thus, xylulose is transported from the high pH to the low pH medium across the contained organic liquid membrane in the device. The transport of xylulose is facilitated through the organic film by the dissolved ABA and QX combination.
As the hydrolysate repeatedly passes through the immobilized XI (or solid acid/base catalyst) column, the extraction of xylulose to the organic phase continues until nearly all of the xylose is isomerized. At the end of the contacting process, xylulose is accumulated in process 36 (unit 4) and glucose remains in the first container 30 (unit 1). By controlling the volume of stripping medium used, the concentration of xylulose can be higher than the initial concentration of xylose in the hydrolysate. The organic phase containing the ABA and the lipophilic ammonium salt can be used repeatedly.
Implementation of Method II—Isomerization Coupled to Selective Solid-Phase Extraction and Stripping
The liquid-liquid extraction and stripping systems described in Method II confine the ABA to the organic phase through the addition of the QX compound.
Another, and simpler, method for confining the sugar complexing agent to a second phase is by binding it to a solid support material. In this way, the immobilized CA acts as a solid-phase extraction medium and the overall process operates in a manner similar to the “isomerization coupled to selective liquid-extraction and stripping” described previously.
By immobilizing the sugar complexing agent to a support material, the property of the CA can also be altered to further enhance its selectivity for a specific sugar and alter the pH range over which this binding occurs. Once a sugar has selectively bound to the immobilized CA, it is effectively removed from the hydrolysate medium. Subsequently, the bound sugar can be dislodged from the CA by flushing the support material with a lower pH solution, thereby achieving its separation from the hydrolysate.
By selecting appropriate complexing species, pH and temperature conditions, the present method uses differences in binding affinity of the CA to specific sugars, and selectively removes a single or multiple sugars from a sugar mixture (such as biomass hydrolysate).
This method has the additional advantage that, following separation, the separated sugar(s) is already in the ketose form that is readily amenable to further chemical conversion. Moreover, the separated sugars can be recovered in the form of concentrated solutions.
Another embodiment of Method II is shown in
The CA and its binding chemistry to the support material are so chosen that at the pH and temperature conditions of the experiment it would only bind to xylulose, and will not bind any appreciable amounts of glucose, xylose or fructose. As the hydrolysate passes through the first (XI) column 51, xylose and a portion of glucose are converted to their corresponding keto-isomers (xylulose and fructose, respectively). As this reaction mixture is routed through the immobilized second (CA) column 52, only the xylulose in the sugar mixture will complex with bound CA sites, thereby lowering the xylulose concentration in the hydrolysate. This reduction of “free xylulose” concentration in the hydrolysate drives the isomerization reaction in the direction of more xylulose formation. This in situ product (xylulose) removal from the reaction mixture allows one to overcome the unfavorable equilibrium ratio of xylose:xylulose for this reaction.
Thus, as the reaction mixture circulates through the two-columns connected in series to the batch vessel 50 containing the hydrolysate, not only will all the xylose in the hydrolysate be converted to xylulose, but it will also attach to the CA in the second (CA) column 52. Hence, at the end of the process, there is a hydrolysate in the batch vessel 50 containing essentially only the C6 sugars.
At this point, the system can be adapted to isolate the immobilized CA column 52 (shown on the right sight of
This method will also regenerate the immobilized CA column which could now be reused with a fresh batch of biomass hydrolysate. The low pH 2 to 4.5 medium used to dislodge bound-xylulose can be pH adjusted slightly following sugar removal to accommodate fermentation of xylulose to ethanol by native S. cerevisiae. By controlling the volume of the carrier solution used to dislodge the bound-xylulose, one can also recover the xylulose solution as a “concentrated” solution. Thus, this method, in addition to separating the xylose from C6 sugars in the form of its keto-isomer, allows us to recover it as a concentrated solution.
The present invention is further defined in the following Examples, in which all parts and percentages are by weight and degrees are Celsius, unless otherwise stated. It should be understood that these Examples, while indicating preferred embodiments of the invention, are given by way of illustration only. From the above discussion and these Examples, one skilled in the art can ascertain the essential characteristics of this invention, and without departing from the spirit and scope thereof, can make various changes and modifications of the invention to adapt it to various usages and conditions. All publications, including patents and non-patent literature, referred to in this specification are expressly incorporated by reference. The following examples are intended to illustrate certain preferred embodiments of the invention and should not be interpreted to limit the scope of the invention as defined in the claims, unless so specified.
The value of the present invention can thus be seen by reference to the Examples herein. The methods described herein provides at least the following: enhancement of xylose isomerization with complexing agents; robust immobilization of XI; identification of specific CAs that can display selective affinity toward xylulose at the pH optimum for immobilized XI (or solid acid/base catalyst); isomerization by immobilized XI particles and enhancement of equilibrium conversion with complexing agents that can phase-switch between aqueous and organic phases; extraction and subsequent stripping of xylulose into (and out of) an organic phase containing a CA and a lipophilic salt; immobilization of ABAs on solid supports to implement solid-phase extraction; and, isomerization coupled to selective solid-phase extraction and stripping.
The inventors herein designed a jacketed packed bed immobilized XI reactor using commercial Gensweet™ particles to assess the performance of complexing agents on xylose isomerization. Isomerization of xylose was conducted at 50° C. using 50 mL of media containing 10 mM Tris buffer and 30 g/L xylose recirculated at 30 ml/min through the packed bed reactor.
While borax as a complexing agent shifts the xylose-xylulose equilibrium towards higher yields of xylulose, due to its water solubility over a wide pH range, borax is not amenable to recovery using the methods described herein. Still, notwithstanding the limitations of borax, the inventors' initial experiments aimed at understanding the role of boronate-ester formation on xylose-xylulose equilibrium shift were conducted with and without borax (50 mM) in the medium. The results of these experiments are summarized in
In the absence of borax, even at the optimum pH (˜7.5-8.5) of the XI the maximum conversion of xylose is less than 30% indicating the extremely unfavorable equilibrium for this reaction. Borax, which preferentially forms boronate esters with xylulose, is able to significantly shift this equilibrium, ultimately reaching near 90% conversion to xylulose. Accordingly, the data in
In this example, novel covalent binding of XI to functionalized supports are used to achieve robustly immobilized XI. The performance of XI on these supports is evaluated in the presence of 50 mM borax for comparison with the commercial pellets.
The data show results for the robust immobilization of XI. Three functionalized commercial supports, namely Eupergit® C250L, Sepabeads® EP, and Sepabeads® HFA, were used. These supports (beads with ˜250 μm diameter) were selected due to their functionalization with oxirane groups and their ability to withstand pH range from 0 to 14 without swelling or shrinking. The oxirane chemistry allows stable covalent binding under mild reaction conditions (neutral and alkaline pH) to several different groups (e.g. amino (primary), hydroxyl, thiol, phenolic and imidazole ones) on enzymes.
Immobilization of soluble XI (SGI, Genencor) on the specific support Sepabeads EP was achieved by contacting excess enzyme in 50 ml of 1.25 M phosphate buffer at pH 8 with 0.94 g beads in a well-stirred batch vessel. Of the three supports, Sepabeads EP provided the most robust immobilization of XI.
Isomerization was conducted in the same manner as in Example 1. To evaluate robustness (longevity of enzyme activity) of the immobilized XI, isomerization experiments were conducted for varying lengths of time over a 14 day period. The transient concentrations of xylose and xylulose in the reaction media were measured using HPLC to determine the kinetics of the isomerization and hence the activity of the immobilized enzyme. XI immobilized on Sepabeads EP shows remarkable stability and retention of XI activity, as shown in
Biomass hydrolysate medium is a mixture of both C6 and C5 sugars. The XI enzyme is capable of catalyzing aldose-ketose transformations of both glucose and xylose. As such, the inventors herein identified CAs that display higher affinity toward xylulose than fructose, as less CA would be required to achieve high xylulose yields. In some applications, such as cellulosic ethanol, glucose-fructose transformations are inconsequential as yeast strains used for fermentation can use either sugar equally. However, yeast cannot ferment xylose to ethanol. For this scenario, CAs selective to xylulose that can be recovered using Method I or Method II.
As shown in
The inventors determined several CAs that are useful for the schemes described in Methods I and II. The tetrahydroxyborate ions derived from borax are able to efficiently bind to ketose sugars as already seen in Example 1 (see, for example, B(OH)4— in
The inventors also observed that hexahydroxygermanate is also an equally efficient inorganic ketose-sugar selective CA (see, for example, Ge(OH)62− in
PBA,
##STR00008##
3aPBA,
##STR00009##
and 4cPBA,
##STR00010##
are aryl boronic acids and, as such, are suitable for implementation in Method I and II. It should be noted that to be useful in solid phase extraction, an additional requirement of the ABA is the presence of a functional group on the benzene ring that serve to tether the ABA to a solid support. The amine and carboxyl groups on 3aPBA and 4cPBA serve this purpose.
The ability of each of these CAs to bind sugar varies with pH. While not wishing to be bound by theory, the inventors herein now believe that as the pH increases the proportion of the CA in the conjugate base form will increase. This shift between conjugate acid and base will depend on the difference between the pKa of the specific CA and the pH. Since only the conjugate base forms the tetragonal boronic acid ester, the unbound xylulose concentration in the aqueous phase decreases with increasing pH, shifting the isomerization equilibrium in favor of more xylulose formation. Each of the compounds tested show a significant increase in xylose conversion in the pH range from 7.5 to 8.5 (data not shown). All the data in
The inventors herein tested the ability of 4cPBA to isomerize xylose in a phase-switching configuration. Appropriate amounts of the organic phase (MIBK) with dissolved 4cPBA, a high pH aqueous phase containing xylose, and immobilized XI pellets were brought together in a shake flask and the three-phase mixture was vigorously stirred overnight. The conversion of xylose to xylulose was compared to a baseline case with the same amount of CA dissolved directly into the aqueous phase at high pH.
4cPBA enhances isomerization by binding to xylulose following its extraction from the MIBK to the aqueous phase. The enhancement seen in this phase-switching mode is within 80% of that seen when it was directly added to the aqueous phase. Results of the experiments are summarized in Table 1 below.
TABLE 1
Initial
composition of
Xylose
Case
CA1
Aqueous Phase
organic phase1
conversion
Notes
1
None
50 ml of 20 mM
None
~28%
Baseline
xylose
conversion w/o
CA
4cPBA
50 ml of 30 mM
None
~70%
Baseline
xylose + 30 mM
conversion w/
4cPBA
4cPBA
4cPBA
50 ml of 20 mM
100 ml of 10 mM
~57%
Conversion w/
xylose
4cPBA in MIBK
4cPBA phase
switching
These experiments illustrate the achievability of phase-switching to enhance xylose isomerization. Immobilized XI was added to the aqueous phase at pH 8 with or without 4cPBA in a shake flask. For the phase switching experiments, the CA was dissolved in methyl-isobutyl-ketone (MIBK) and the immiscible organic phase was mixed vigorously with the aqueous sugar solution. Experiments were run overnight to ensure equilibrium conversion. The CA to xylose molar ratios used was 1:1.
4cPBA does not dissolve in aqueous solution at low pH. Accordingly, lowering the pH of the shake flask contents at the end of the experiment will release the xylulose bound to the 4cPBA and 4cPBA will migrate back to the MIBK phase, leaving free xylulose behind. Thus, this experiment provides proof for the phase-switching method of enhancing isomerization of xylose by the CA.
Addition of a lipophilic ammonium salt QX to the organic phase along with ABA prevents the migration of ABA into the aqueous phase even at high pH. Instead, the xylulose is extracted into the organic phase as described in Method II. In this embodiment, removal of xylulose from the aqueous medium drives the isomerization towards more xylulose formation. Further, contacting the organic phase with a small quantity of a low pH aqueous stripping solution will release the xylulose into the aqueous medium as a concentrated sugar solution (see Table 2 below). This mode of operation corresponds to liquid-liquid extraction followed by stripping (Method II). These data also form the basis for the implementation of Method II in a HFCLMC configuration.
Further experiments, as shown in Table 2 below, illustrate the achievability of extraction followed by stripping to enhance xylose isomerization and recovery.
TABLE 2
Initial composition
Composition of extracted
CA
aqueous phase
of organic phase
sugar solution
None
50 ml of
None
~28% xylulose
20 mM xylose
N2B
100 ml of
100 ml of n-hexane/
~77% xylulose
20 mM xylose
1-octanol, 150 mM
Aliquat ® 336, N2B
These experiments illustrate the achievability of extraction followed by stripping to enchance xylose isomerization and recovery. Immobilized XI was added to the aqueous phase at pH 8.5 with or without naphthalene-2-boronic acid (N2B) in shake flask. For the extraction experiments, the N2B was dissolved in an 85:15 v/v ratio of n-hexane to 1-octanol containing 150 mM Aliquat ® 336. The immiscible organic phase was mixed vigorously with the aqueous sugar solution for 9 hrs. The stripping experiments were run by contacting the sugar-laden organic phase with 0.5 M HCl (pH ~ 0.3) for 30 mins, The N2B-to-sugar molar ratios tested were ≧ 2.5:1.
As noted in Example 3, both 4cPBA and 3aPBA possess pendant groups that enable their attachment to a functionalized solid support. The Sepabead® EP beads used for the immobilization of XI also form a suitable support for immobilization of 3aPBA. The oxirane group on the support covalently bonds the amine group of the 3aPBA by epoxide ring-opening as shown in
Through experiments performed over a range of pH values and sodium phosphate buffer concentrations, the inventors determined that the useful conditions for immobilization of 3aPBA on the Sepabead® EP were pH 8 and 1 M sodium phosphate buffer at 25° C. In one embodiment, Sepabead® EP beads were contacted with the buffer containing 3aPBA in a molar ratio of oxirane to amine of 1:2 for 24 hrs. Binding of 3aPBA was followed indirectly by monitoring the concentration of 3aPBA in the buffer with UV absorbance spectroscopy at 295 nm. At the end of the experiment, the beads were washed thoroughly with DI water to remove any non-covalently associated 3aPBA. Based on mass balances, it was determined that under the conditions specified, all of the oxirane sites were covalently attached to 3aPBA.
The inventors investigated the affinity of the immobilized CA to the four sugars: glucose, fructose, xylose and xylulose.
In biomass hydrolysate glucose and xylose are the two predominant C6 and C5 sugars; when the hydrolysate at a pH of 9 is circulated through an immobilized CA column, both sugars bind to CA to about the same extent (see
However, if the hydrolysate is passed through an immobilized xylose isomerase (XI) column prior to the CA column (see
As can be seen from the schematic illustration shown in
Using the Method II illustrated in
As shown in
While the invention has been described with reference to various and preferred embodiments, it should be understood by those skilled in the art that various changes may be made and equivalents may be substituted for elements thereof without departing from the essential scope of the invention. In addition, many modifications may be made to adapt a particular situation or material to the teachings of the invention without departing from the essential scope thereof.
Therefore, it is intended that the invention not be limited to the particular embodiment disclosed herein contemplated for carrying out this invention, but that the invention will include all embodiments falling within the scope of the claims.
Li, Bin, Varanasi, Sasidhar, Relue, Patricia
| Patent | Priority | Assignee | Title |
| Patent | Priority | Assignee | Title |
| 3793189, | |||
| 4069104, | Jun 17 1975 | Imperial Chemical Industries Limited | Conversion of aldose to ketose in the presence of oxyanions or mixed oxyanions of tin or germanium |
| 4273922, | Mar 21 1980 | The United States of America as represented by the Secretary of | Ketose sugars from aldose sugars |
| 4490468, | Apr 23 1980 | Purdue Research Foundation | Production of ethanol by yeast using xylulose |
| 5241087, | Mar 09 1992 | Bend Research, Inc. | Enantiomeric enrichment of cyanohydrins |
| 5254468, | Oct 31 1991 | The University of Toledo | Bilayer pellet containing immobilized xylose isomerase and urease for the simultaneous isomerization and fermentation of xylose to ethanol |
| 5397700, | Oct 31 1991 | University of Toledo | Method of producing products with a bilayer pellet containing a coimmobilized enzyme system that maintains a ph difference |
| 5800624, | Oct 22 1996 | University of Notre Dame | Membrane process for separating carbohydrates |
| 5840677, | Jul 09 1993 | NOVOZYMES A S | Boronic acid or borinic acid derivatives as enzyme stabilizers |
| 6022477, | Nov 14 1997 | New Jersey Institute of Technology | Method and apparatus for isolation purification of biomolecules |
| 7037378, | Sep 24 2003 | Danisco Sweeteners Oy | Separation of sugars |
| 7674608, | Feb 23 2007 | The University of Toledo | Saccharifying cellulose |
| 8217211, | Aug 27 2007 | Purdue Research Foundation | Process for producing liquid hydrocarbon by pyrolysis of biomass in presence of hydrogen from a carbon-free energy source |
| 8507232, | Jan 04 2008 | The University of Toledo | Methods for fermentation of xylose and hexose sugars |
| 8927240, | Nov 12 2010 | The University of Toledo | Thermal fractionation of biomass of non-lignocellulosic origin for multiple high-quality biofuels |
| 20080227162, | |||
| 20080241818, | |||
| 20080318284, | |||
| 20090011473, | |||
| 20090082604, | |||
| 20090090046, | |||
| 20090139137, | |||
| 20090275098, | |||
| 20090305935, | |||
| 20100004437, | |||
| 20100269990, | |||
| 20100285552, | |||
| 20110294163, | |||
| 20130074397, | |||
| WO2005056808, | |||
| WO2009089103, |
| Executed on | Assignor | Assignee | Conveyance | Frame | Reel | Doc |
| Apr 19 2011 | The University of Toledo | (assignment on the face of the patent) | / | |||
| Jun 23 2011 | University of Toledo | UNITED STATE DEPARTMENT OF ENERGY | CONFIRMATORY LICENSE SEE DOCUMENT FOR DETAILS | 026979 | /0631 | |
| Nov 05 2012 | RELUE, PATRICIA | The University of Toledo | ASSIGNMENT OF ASSIGNORS INTEREST SEE DOCUMENT FOR DETAILS | 029278 | /0465 | |
| Nov 05 2012 | LI, BIN | The University of Toledo | ASSIGNMENT OF ASSIGNORS INTEREST SEE DOCUMENT FOR DETAILS | 029278 | /0465 | |
| Nov 06 2012 | VARANASI, SASIDHAR | The University of Toledo | ASSIGNMENT OF ASSIGNORS INTEREST SEE DOCUMENT FOR DETAILS | 029278 | /0465 | |
| Jul 19 2018 | University of Toledo | United States Department of Energy | CONFIRMATORY LICENSE SEE DOCUMENT FOR DETAILS | 048589 | /0891 |
| Date | Maintenance Fee Events |
| Jul 26 2019 | M2551: Payment of Maintenance Fee, 4th Yr, Small Entity. |
| Jul 26 2023 | M2552: Payment of Maintenance Fee, 8th Yr, Small Entity. |
| Date | Maintenance Schedule |
| Jan 26 2019 | 4 years fee payment window open |
| Jul 26 2019 | 6 months grace period start (w surcharge) |
| Jan 26 2020 | patent expiry (for year 4) |
| Jan 26 2022 | 2 years to revive unintentionally abandoned end. (for year 4) |
| Jan 26 2023 | 8 years fee payment window open |
| Jul 26 2023 | 6 months grace period start (w surcharge) |
| Jan 26 2024 | patent expiry (for year 8) |
| Jan 26 2026 | 2 years to revive unintentionally abandoned end. (for year 8) |
| Jan 26 2027 | 12 years fee payment window open |
| Jul 26 2027 | 6 months grace period start (w surcharge) |
| Jan 26 2028 | patent expiry (for year 12) |
| Jan 26 2030 | 2 years to revive unintentionally abandoned end. (for year 12) |